CN105750090B - A kind of silicon calcium collophanite method for separating - Google Patents
A kind of silicon calcium collophanite method for separating Download PDFInfo
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- CN105750090B CN105750090B CN201610300010.6A CN201610300010A CN105750090B CN 105750090 B CN105750090 B CN 105750090B CN 201610300010 A CN201610300010 A CN 201610300010A CN 105750090 B CN105750090 B CN 105750090B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
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Abstract
The present invention relates to a kind of silicon calcium collophanite method for separating.Its technical scheme is：Silicon calcium collophanite is crushed, it is to account for 50 ~ 90wt% less than 0.074mm to be finely ground to granularity, adjusts to ore pulp, gravity treatment, obtains gravity concentrate and gravity tailings.The gravity concentrate is adjusted to ore pulp, lauryl sodium sulfate is added and carries out reverse flotation dolomite, obtain concentrate I and chats.The gravity tailings is adjusted to ore pulp, sequentially adds sodium carbonate, waterglass and fatty-acid collector, direct flotation is carried out, obtains rough concentrate and mine tailing I.By the rough concentrate and the chats in mass ratio（2~8）: 1 merges, and adjusts to ore pulp, sequentially adds regulator and fatty-acid collector, carries out reverse flotation, obtained concentrate II.The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product.The present invention has the advantages of ore strong adaptability, good separation effect, floating agent consumption is small, beneficiation cost is low and environmental pollution is small.
Description
Technical field
The invention belongs to collophane sorting technology field.More particularly to a kind of silicon calcium collophanite method for separating.
Background technology
Though China's phosphate rock resource rich reserves, P2O5Average grade is only 16.95%, P2O5Grade is more than 30% rich ore
Only account for 6.75%.As rich phosphorus ore and Yi Xuan phosphate rock resources are increasingly reduced, the mineral processing technology of silicon calcium collophanite is studied especially
To be important.At present, flotation of phosphate rock method mainly has floatation, scrubbing-desliming method, gravity separation method, roasting-digestion method, chemistry leaching
Method, photoelectric separation method and beneficiation combined method method etc., the sorting process maximally efficient to silicon calcium collophanite is floatation, main bag
Include direct-reverse flotation method, trans- direct flotation method and bi-anti-symmetric matrix method.Though floatation is current most widely used maximally efficient method,
Still suffer from the problem of floating agent consumption is big, beneficiation cost is high and environmental pollution is serious.Therefore, to silicon calcium collophanite grder man
Skill, which optimizes, to be significant.
Fourth great waves（Fourth great waves, red appositional patterns silicon calcium quality ore stone gravity treatment preconcentration experimental study [J] the Guizhou of Liu Zhi
Chemical industry, 2013,38（3））Using appositional pattern silicon calcium quality ore stone as research object, shaking table is respectively adopted and chute carries out pre- getting rich first
Collection experiment, the results showed that, chute sorts the effect for preferably, having reached preconcentration to appositional pattern silicon calcium quality ore stone, makes impurity
SiO2It is relative to be enriched in mine tailing, flotation treating capacity, simplification of flowsheet can be reduced.But the phosphorus that the preenrichment technique obtains
Concentrate content of MgO is high, and ore adaptability is not strong.
" a kind of collophane direct reverse flotation technique "（CN 1730161 A）Patented technology, first mill head is top-uped
Choosing, flotation froth product is then aligned again and carries out reverse flotation, product is as concentrate product in gained groove.Though the technique overcomes just
Alkali consumption present in flotation phosphate mineral processes is big and flotation pulp temperature is high（More than 42 DEG C）The problem of, but still suffer from positive and negative floating
Select the defects of throughput is big, reverse flotation acid consumption is big and environmental pollution is serious.
" a kind of branch flotation technology for silicon calcium collophanite "（CN 102744151 A）Patented technology, first to selected original
Ore deposit carries out reverse flotation, is then classified concentrate through reverse flotation, then carries out Counterfloatating desiliconization to coarse fraction part respectively, to particulate
Level part carries out direct-flotation desiliconisation, and product and direct flotation froth pulp are incorporated as phosphorus concentrate production in gained Counterfloatating desiliconization groove
Product.Though the technique overcomes bi-anti-symmetric matrix except silicon operation phosphorus concentrate grade improves the shortcomings that limited, reverse flotation consumption acid is still suffered from
The shortcomings that amount is greatly and beneficiation cost is high.
In summary, though existing silicon calcium collophanite sorting process separating effect is preferable, choosing is reduced to a certain extent
Ore deposit cost, but still suffer from the defects of ore adaptability is not strong, floating agent consumption is big and beneficiation cost is high.
The content of the invention
It is contemplated that prior art defect is overcome, and it is an object of the present invention to provide a kind of ore strong adaptability, good separation effect, floating
Select the silicon calcium collophanite method for separating that reagent consumption is small, beneficiation cost is low and environmental pollution is small.
To achieve the above object, the technical solution adopted by the present invention comprises the concrete steps that：
（1）Silicon calcium collophanite is crushed, granularity is finely ground to and accounts for 50 ~ 90wt% less than 0.074mm, obtain ore milling product, then
The ore milling product is adjusted to the ore pulp that concentration is 10 ~ 30wt%, gravity treatment, obtains gravity concentrate and gravity tailings.
（2）The gravity concentrate is adjusted to the ore pulp that concentration is 25 ~ 40wt%, is sent into tank diameter I, then add into tank diameter I
Enter lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.1 ~ 1.0kg；Reverse flotation is carried out again
Dolomite operation, product I and froth pulp I in groove are obtained, product I is concentrate I in groove, in being after the dehydration of froth pulp I
Ore deposit.
（3）The gravity tailings is adjusted to the ore pulp that concentration is 20 ~ 35wt%, is sent into tank diameter II, then into tank diameter II
Sequentially add sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and aliphatic acid collecting in gravity tailings per ton
Agent addition is correspondingly 2 ~ 4kg, 0.2 ~ 2.0kg and 0.6 ~ 1.6kg；Direct flotation operation is carried out again, obtains the He of product II in groove
Froth pulp II, product II is mine tailing I in groove, froth pulp II be dehydrated after be rough concentrate.
（4）By the rough concentrate: the mass ratio of the chats is（2~8）: 1 matches somebody with somebody ore deposit, obtains composite ore, by the composite ore
The ore pulp that concentration is 20 ~ 35wt% is adjusted to, is sent into tank diameter III, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 3 ~ 11kg and 0.1 ~ 0.8kg；Carry out again
Reverse flotation work, product III and froth pulp III in groove are obtained, product is concentrate II in groove, and froth pulp is mine tailing II.
（5）The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product, by the mine tailing I and the mine tailing II
Merge, obtain phosphorus product from failing.
The silicon calcium collophanite P2O5Grade is that 20 ~ 28%, MgO grades are 1 ~ 6%.
The gravity treatment is one kind in sluicing, separation by shaking table, dense medium separation and hydrocyclone sorting.
The regulator is one or both of sulfuric acid and phosphoric acid.
The present invention compared with prior art, has the positive effect that：
1st, the present invention is applied to P2O5The silicon calcium collophanite that grade is 20 ~ 28wt%, MgO grades are 1 ~ 6wt%, ore are fitted
Ying Xingqiang.
2nd, the present invention uses lauryl sodium sulfate as dolomite collecting agent reverse flotation dolomite, without adding any adjustment
Agent, has that reagent consumption is small and the obvious advantage of separating effect.
3rd, the present invention use reselecting method and reverse flotation dolomite method, can Pre-sorting go out 30 ~ 60% qualified phosphorus concentrates, greatly
The treating capacity of follow-up direct-reverse flotation is reduced greatly, reduces the consumption of floating agent, is reduced beneficiation cost and is protected ring
Border.
4th, the phosphorus concentrate product P that the present invention is obtained2O5Grade is less than 1%, P more than 30% and MgO grades2O5The rate of recovery is big
In 80%.
Therefore, the present invention has ore strong adaptability, good separation effect, floating agent consumption is small, beneficiation cost is low and ring
The characteristics of border pollution is small.
Brief description of the drawings
Fig. 1 be the present invention in sluicing used in screening installation a kind of structural representation；
Fig. 2 is the schematic diagram of Fig. 1 horizontal wash tub pipe 8.
Embodiment
For a better understanding of the present invention, present disclosure is described further with reference to embodiment, but this
The content of invention is not limited solely to the following examples.Any simple modification that all substantive contents according to the present invention are made and
Equivalent structure transformation or modification, it all should be included within the scope of the present invention.
Embodiment 1
A kind of silicon calcium collophanite method for separating.Silicon calcium collophanite P described in the present embodiment2O5Grade is 26 ~ 28%, MgO
Grade is 1 ~ 3%.
The technical scheme that the present embodiment uses comprises the concrete steps that：
（1）Silicon calcium collophanite is crushed, granularity is finely ground to and accounts for 50 ~ 65wt% less than 0.074mm, obtain ore milling product, then
The ore milling product is adjusted to the ore pulp that concentration is 20 ~ 30wt%, gravity treatment, obtains gravity concentrate and gravity tailings.
（2）The gravity concentrate is adjusted to the ore pulp that concentration is 35 ~ 40wt%, is sent into tank diameter I, then add into tank diameter I
Enter lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.1 ~ .5kg；Reverse flotation is carried out again
Dolomite operation, product I and froth pulp I in groove are obtained, product I is concentrate I in groove, in being after the dehydration of froth pulp I
Ore deposit.
（3）The gravity tailings is adjusted to the ore pulp that concentration is 30 ~ 35wt%, is sent into tank diameter II, then into tank diameter II
Sequentially add sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and aliphatic acid collecting in gravity tailings per ton
Agent addition is correspondingly 2 ~ 3kg, 0.2 ~ 0.8kg and 0.6 ~ 1.0kg；Direct flotation operation is carried out again, obtains the He of product II in groove
Froth pulp II, product II is mine tailing I in groove, froth pulp II be dehydrated after be rough concentrate.
（4）By the rough concentrate: the mass ratio of the chats is（2~5）: 1 matches somebody with somebody ore deposit, obtains composite ore, by the composite ore
The ore pulp that concentration is 25 ~ 35wt% is adjusted to, is sent into tank diameter III, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 3 ~ 6kg and 0.1 ~ 0.3kg；Carry out again
Reverse flotation work, product III and froth pulp III in groove are obtained, product is concentrate II in groove, and froth pulp is mine tailing II.
（5）The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product, by the mine tailing I and the mine tailing II
Merge, obtain phosphorus product from failing.
Gravity treatment described in the present embodiment is dense medium separation.
Regulator described in the present embodiment is phosphoric acid.
The present embodiment uses reselecting method and reverse flotation dolomite method, can Pre-sorting go out 45 ~ 60% qualified phosphorus concentrates；Institute
The phosphorus concentrate product P of acquisition2O5Grade is less than 1%, P more than 30% and MgO grades2O5The rate of recovery is more than 90%.
Embodiment 2
A kind of silicon calcium collophanite method for separating.Silicon calcium collophanite P described in the present embodiment2O5Grade is 24 ~ 26%, MgO
Grade is 2 ~ 4%.
The technical scheme that the present embodiment uses comprises the concrete steps that：
（1）Silicon calcium collophanite is crushed, granularity is finely ground to and accounts for 55 ~ 70wt% less than 0.074mm, obtain ore milling product, then
The ore milling product is adjusted to the ore pulp that concentration is 15 ~ 25wt%, gravity treatment, obtains gravity concentrate and gravity tailings.
（2）The gravity concentrate is adjusted to the ore pulp that concentration is 28 ~ 32wt%, is sent into tank diameter I, then add into tank diameter I
Enter lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.3 ~ 0.7kg；Reverse flotation is carried out again
Dolomite operation, product I and froth pulp I in groove are obtained, product I is concentrate I in groove, in being after the dehydration of froth pulp I
Ore deposit.
（3）The gravity tailings is adjusted to the ore pulp that concentration is 28 ~ 32wt%, is sent into tank diameter II, then into tank diameter II
Sequentially add sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and aliphatic acid collecting in gravity tailings per ton
Agent addition is correspondingly 2.5 ~ 3.5kg, 0.6 ~ 1.4kg and 0.8 ~ 1.2kg；Direct flotation operation is carried out again, obtains product in groove
II and froth pulp II, product II is mine tailing I in groove, froth pulp II be dehydrated after be rough concentrate.
（4）By the rough concentrate: the mass ratio of the chats is（3~6）: 1 matches somebody with somebody ore deposit, obtains composite ore, by the composite ore
The ore pulp that concentration is 20 ~ 30wt% is adjusted to, is sent into tank diameter III, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 4 ~ 7kg and 0.2 ~ 0.5kg；Carry out again
Reverse flotation work, product III and froth pulp III in groove are obtained, product is concentrate II in groove, and froth pulp is mine tailing II.
（5）The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product, by the mine tailing I and the mine tailing II
Merge, obtain phosphorus product from failing.
Gravity treatment described in the present embodiment is separation by shaking table.
Regulator described in the present embodiment is the mixture of sulfuric acid and phosphoric acid.
The present embodiment uses reselecting method and reverse flotation dolomite method, can Pre-sorting go out 35 ~ 50% qualified phosphorus concentrates；Institute
The phosphorus concentrate product P of acquisition2O5Grade is less than 1%, P more than 30% and MgO grades2O5The rate of recovery is more than 85%.
Embodiment 3
A kind of silicon calcium collophanite method for separating.Silicon calcium collophanite P described in the present embodiment2O5Grade is 22 ~ 24%, MgO
Grade is 3 ~ 5%.
The technical scheme that the present embodiment uses comprises the concrete steps that：
（1）Silicon calcium collophanite is crushed, granularity is finely ground to and accounts for 60 ~ 85wt% less than 0.074mm, obtain ore milling product, then
The ore milling product is adjusted to the ore pulp that concentration is 10 ~ 20wt%, gravity treatment, obtains gravity concentrate and gravity tailings.
（2）The gravity concentrate is adjusted to the ore pulp that concentration is 25 ~ 35wt%, is sent into tank diameter I, then add into tank diameter I
Enter lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.5 ~ 1.0kg；Reverse flotation is carried out again
Dolomite operation, product I and froth pulp I in groove are obtained, product I is concentrate I in groove, in being after the dehydration of froth pulp I
Ore deposit.
（3）The gravity tailings is adjusted to the ore pulp that concentration is 20 ~ 25wt%, is sent into tank diameter II, then into tank diameter II
Sequentially add sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and aliphatic acid collecting in gravity tailings per ton
Agent addition is correspondingly 2.5 ~ 4.0kg, 0.8 ~ 1.6kg and 1.0 ~ 1.4kg；Direct flotation operation is carried out again, obtains product in groove
II and froth pulp II, product II is mine tailing I in groove, froth pulp II be dehydrated after be rough concentrate.
（4）By the rough concentrate: the mass ratio of the chats is（4~7）: 1 matches somebody with somebody ore deposit, obtains composite ore, by the composite ore
The ore pulp that concentration is 20 ~ 30wt% is adjusted to, is sent into tank diameter III, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 5 ~ 9kg and 0.3 ~ 0.7kg；Carry out again
Reverse flotation work, product III and froth pulp III in groove are obtained, product is concentrate II in groove, and froth pulp is mine tailing II.
（5）The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product, by the mine tailing I and the mine tailing II
Merge, obtain phosphorus product from failing.
Gravity treatment described in the present embodiment is sluicing, and equipment is a kind of " sulfuric acid residual separating-purifying used by sluicing
Screening installation "（CN200410060867.2）.The structure such as Fig. 1 and Fig. 2 of " a kind of sulfuric acid residual separating-purifying-sorting apparatus "
It is shown, mine distributor 1 is fixedly connected and on upper bracket 2 with feed launder 3, upper bracket 2 is fixed with helicla flute pillar 4 to be connected
Connect, spiral chute 5 is fixedly connected with helicla flute pillar 4, and the upper end of spiral chute 5 is located under upper bracket 2, lower end and mine cut groove 6
Connect, mine cut groove 6 and connect ore bucket 7 and connect, horizontal wash tub pipe 8, horizontal wash tub pipe 8 are provided with the inner side of spiral chute 5
External high-pressure water, some apopores are provided with the inner side of horizontal wash tub pipe 8, and horizontal wash tub pipe 8 is shaped as tube auger
Shape.
For the spiral chute 5 that the present embodiment uses for 3, sectional curve uses compound cubic parabola sectional curve, top
Oblique angle is more than bottom under the transverse direction of sectional curve.The ratio between the high h of flight and outer diameter D are：H/D=0.35.Spiral chute 5 is by glass
Fibre reinforced plastics or fiberglass are made, and liner is corundum type high-abrasive material.
Regulator described in the present embodiment is sulfuric acid.
The present embodiment uses reselecting method and reverse flotation dolomite method, can Pre-sorting go out 30 ~ 50% qualified phosphorus concentrates；Institute
The phosphorus concentrate product P of acquisition2O5Grade is less than 1%, P more than 30% and MgO grades2O5The rate of recovery is more than 80%.
Embodiment 4
A kind of silicon calcium collophanite method for separating.Silicon calcium collophanite P described in the present embodiment2O5Grade is 20 ~ 22%, MgO
Grade is 4 ~ 6%.
The technical scheme that the present embodiment uses comprises the concrete steps that：
（1）Silicon calcium collophanite is crushed, granularity is finely ground to and accounts for 70 ~ 90wt% less than 0.074mm, obtain ore milling product, then
The ore milling product is adjusted to the ore pulp that concentration is 10 ~ 20wt%, gravity treatment, obtains gravity concentrate and gravity tailings.
（2）The gravity concentrate is adjusted to the ore pulp that concentration is 25 ~ 30wt%, is sent into tank diameter I, then add into tank diameter I
Enter lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.7 ~ 1.0kg；Reverse flotation is carried out again
Dolomite operation, product I and froth pulp I in groove are obtained, product I is concentrate I in groove, in being after the dehydration of froth pulp I
Ore deposit.
（3）The gravity tailings is adjusted to the ore pulp that concentration is 23 ~ 28wt%, is sent into tank diameter II, then into tank diameter II
Sequentially add sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and aliphatic acid collecting in gravity tailings per ton
Agent addition is correspondingly 3 ~ 4kg, 1.0 ~ 2.0kg and 1.0 ~ 1.6kg；Direct flotation operation is carried out again, obtains the He of product II in groove
Froth pulp II, product II is mine tailing I in groove, froth pulp II be dehydrated after be rough concentrate.
（4）By the rough concentrate: the mass ratio of the chats is（5~8）: 1 matches somebody with somebody ore deposit, obtains composite ore, by the composite ore
The ore pulp that concentration is 20 ~ 25wt% is adjusted to, is sent into tank diameter III, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 6 ~ 11kg and 0.5 ~ 0.8kg；Carry out again
Reverse flotation work, product III and froth pulp III in groove are obtained, product is concentrate II in groove, and froth pulp is mine tailing II.
（5）The concentrate I and the concentrate II are merged, obtain phosphorus concentrate product, by the mine tailing I and the mine tailing II
Merge, obtain phosphorus product from failing.
Gravity treatment described in the present embodiment sorts for hydrocyclone.
Regulator described in the present embodiment is sulfuric acid.
The present embodiment uses reselecting method and reverse flotation dolomite method, can Pre-sorting go out 30 ~ 45% qualified phosphorus concentrates；Institute
The phosphorus concentrate product P of acquisition2O5Grade is less than 1%, P more than 30% and MgO grades2O5The rate of recovery is more than 80%.
Present embodiment compared with prior art, has the positive effect that：
1st, present embodiment is applied to P2O5The silico-calcium matter glue phosphorus that grade is 20 ~ 28wt%, MgO grades are 1 ~ 6wt%
Ore deposit, ore strong adaptability.
2nd, present embodiment uses lauryl sodium sulfate as dolomite collecting agent reverse flotation dolomite, without adding
Any regulator, has that reagent consumption is small and the obvious advantage of separating effect.
3rd, present embodiment uses reselecting method and reverse flotation dolomite method, can Pre-sorting go out 30 ~ 60% qualified phosphorus
Concentrate, the treating capacity of follow-up direct-reverse flotation is greatly reduced, reduce the consumption of floating agent, reduced beneficiation cost and protect
Environment is protected.
4th, the phosphorus concentrate product P that present embodiment is obtained2O5Grade is less than 1%, P more than 30% and MgO grades2O5
The rate of recovery is more than 80%.
Therefore, present embodiment have ore strong adaptability, good separation effect, floating agent consumption be small, ore dressing into
The characteristics of this low and environmental pollution is small.
Claims (4)
1. a kind of silicon calcium collophanite method for separating, it is characterised in that methods described comprises the concrete steps that：
(1) silicon calcium collophanite is crushed, is finely ground to granularity and accounts for 50~90wt% less than 0.074mm, obtain ore milling product, then will
The ore milling product is adjusted to the ore pulp that concentration is 10~30wt%, gravity treatment, obtains gravity concentrate and gravity tailings；
(2) gravity concentrate is adjusted to the ore pulp that concentration is 25~40wt%, is sent into tank diameter I, then add into tank diameter I
Lauryl sodium sulfate, the lauryl sodium sulfate addition in gravity concentrate per ton is 0.1~1.0kg；Reverse flotation is carried out again
Dolomite operation, concentrate I and froth pulp I are obtained, be chats after the dehydration of froth pulp I；
(3) by the gravity tailings be adjusted to concentration be 20~35wt% ore pulp, be sent into tank diameter II, then into tank diameter II according to
Secondary addition sodium carbonate, waterglass and fatty-acid collector, sodium carbonate, waterglass and fatty-acid collector in gravity tailings per ton
Addition is correspondingly 2~4kg, 0.2~2.0kg and 0.6~1.6kg；Direct flotation operation is carried out again, obtains mine tailing I and foam
Product II, it is rough concentrate after the dehydration of froth pulp II；
(4) rough concentrate is pressed: the mass ratio of the chats is (2~8): 1 matches somebody with somebody ore deposit, obtains composite ore, the composite ore is adjusted
To the ore pulp that concentration is 20~35wt%, tank diameter III is sent into, then sequentially add regulator into tank diameter III and aliphatic acid is caught
Agent is received, the regulator and fatty-acid collector addition in composite ore per ton are correspondingly 3~11kg and 0.1~0.8kg；Enter again
Row reverse flotation work, obtains concentrate II and froth pulp III, and froth pulp is mine tailing II；
(5) concentrate I and the concentrate II are merged, obtains phosphorus concentrate product, the mine tailing I and the mine tailing II are closed
And obtain phosphorus product from failing.
2. silicon calcium collophanite method for separating according to claim 1, it is characterised in that the silicon calcium collophanite P2O5Product
Position is that 20~28%, MgO grades are 1~6%.
3. silicon calcium collophanite method for separating according to claim 1, it is characterised in that the gravity treatment is sluicing, shaken
One kind in bed sorting, dense medium separation and hydrocyclone sorting.
4. silicon calcium collophanite method for separating according to claim 1, it is characterised in that the regulator is sulfuric acid and phosphorus
One or both of acid.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105834005A (en) * | 2016-03-25 | 2016-08-10 | 北京矿冶研究总院 | Separation method of mica and feldspar and beneficiation reagent |
| CN108115185B (en) * | 2016-11-17 | 2019-10-29 | 江苏锡沂钢模有限公司 | A kind of milling machine structure |
| CN107335531A (en) * | 2017-09-13 | 2017-11-10 | 化工部长沙设计研究院 | A kind of method of separation by shaking table phosphorus ore |
| CN114011585B (en) * | 2021-10-29 | 2024-03-29 | 宜都兴发化工有限公司 | Flotation method for fine-grained collophanite in gravity tailings |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4189103A (en) * | 1978-03-10 | 1980-02-19 | International Minerals & Chemical Corporation | Method of beneficiating phosphate ores |
| CN1322934C (en) * | 2005-07-30 | 2007-06-27 | 中蓝连海设计研究院 | Collophanite direct flotation and reverse flotation technique |
| CN100522374C (en) * | 2006-01-27 | 2009-08-05 | 湖北宜化肥业有限公司 | Mineral dressing method of mid-low grade collophane |
| CN102671758B (en) * | 2012-05-16 | 2013-06-12 | 云南三明鑫疆矿业有限公司 | Direct and reverse flotation desliming process of collophanite |
| CN102716799A (en) * | 2012-06-14 | 2012-10-10 | 昆明川金诺化工股份有限公司 | Process method for removing phosphate impurities by combining gravity, centrifugal force and flotation |
| CN102744151B (en) * | 2012-07-06 | 2013-09-04 | 中蓝连海设计研究院 | Branch flotation technology for silicon calcium collophanite |
| CN104959239B (en) * | 2015-06-26 | 2017-06-27 | 中国地质科学院矿产综合利用研究所 | Low-grade refractory weathered collophanite segmented desliming flotation process |
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